METHOD FOR CONTINUOUS THERMAL SEPARATION OF A MULTI-COMPONENT SUBSTANCE

Abstract

A method for thermal separation of a substance flowing into a treatment chamber by use of a separation apparatus includes a vessel and a heating device. The vessel has a vessel wall with an inner surface enclosing a treatment chamber of a length l.sub.c, a height H and a width W. The vessel includes at least one substance inlet and at least one first outlet and at least one second outlet for non-evaporable and evaporable parts, respectively. The heating device is arranged outside the treatment chamber and a rotary mechanism includes a rotatable axle arranged within the treatment chamber directed along the treatment chamber's length h and a mixing device of radial diameter d.sub.md and axial length I.sub.md fixed to the rotatable axle and extending perpendicular to the rotatable axle. The method includes: A. heating the inner surface (la) by use of the heating device to transfer thermal energy to a minimum peripheral volume (V.sub.p) of the treatment chamber confined between the mixing device and the inner surface (la), B. rotating the rotary mechanism by use of a rotary drive operably fixed to the rotatable axle to a peripheral rotation velocity (v.sub.p) measured at a radial outer boundary of the mixing device's which exceeds a minimum peripheral rotation velocity (v.sub.p,mm) of 5 meters per second, C. feeding the substance into the treatment chamber through the at least one substance inlet using a feeding device, wherein the substance includes two or more components, where at least one of the components is evaporable at an evaporation temperature (T.sub.e), and D. adjusting at least one of an input power of the heating device, the flow of the substance fed into at least one of the at least one substance inlet, an input power of the rotary drive and an output flow of a non-evaporated part of the substance released from the at least one first outlet, such that a total thermal energy transferred into at least part of the minimum peripheral volume (V.sub.p) results in an operational temperature (T.sub.op) that exceeds the evaporation temperature (T.sub.e) during operation, and wherein the amount of thermal energy transferred into the part of the minimum peripheral volume (V.sub.p) by the heating device constitutes more than 60% of the total thermal energy transferred.

Claims

1. A method for thermal separation of a substance flowing into a treatment chamber by use of a separation apparatus, wherein the separation apparatus comprises: a vessel having vessel wall with an inner surface (la) enclosing a treatment chamber of a length l.sub.e, a height H and a width W, the vessel comprising at least one substance inlet and at least one first outlet and at least one second outlet for non-evaporable and evaporable parts, respectively, a heating device arranged outside the treatment chamber and a rotary mechanism comprising a rotatable axle arranged within the treatment chamber directed along the treatment chamber's length h and a mixing device of radial diameter d.sub.md and axial length I.sub.md fixed to the rotatable axle and extending perpendicular to the rotatable axle, wherein the method comprises: A. heating the inner surface (la) by use of the heating device to transfer thermal energy to a minimum peripheral volume (V.sub.p) of the treatment chamber confined between the mixing device and the inner surface, B. rotating the rotary mechanism by use of a rotary drive operably fixed to the rotatable axle to a peripheral rotation velocity (v.sub.p) measured at a radial outer boundary of the mixing device's which exceeds a minimum peripheral rotation velocity (v.sub.p,mm) of 5 meters per second, C. feeding the substance into the treatment chamber through the at least one substance inlet using a feeding device, wherein the substance comprises two or more components, where at least one of the components is evaporable at an evaporation temperature (T.sub.e), and D. adjusting at least one of: an input power of the heating device, the flow of the substance fed into at least one of the at least one substance inlet, an input power of the rotary drive, and an output flow of a non-evaporated part of the substance released from the at least one first outlet, such that a total thermal energy transferred into at least part of the minimum peripheral volume (V.sub.p) results in an operational temperature (T.sub.op) that exceeds the evaporation temperature (T.sub.e) during operation, and wherein the amount of thermal energy transferred into the part of the minimum peripheral volume (V.sub.p) by the heating device constitutes more than 60% of the total thermal energy transferred, wherein the total transferred thermal energy, combined with rotation of the rotary mechanism, creates a vapor cloud comprising a mixture of the non-evaporable and evaporable parts, resulting in a near instantaneous heating and evaporation within the minimum peripheral volume (V.sub.p).

2. The method according to claim 1, wherein an outermost radial part of the mixing device comprises a plurality of radially separated mixing protrusions.

3. The method according to claim 2, wherein the plurality of radially separated mixing protrusions is divided into one or more sets distributed axially along the rotatable axle, across the axial length (l.sub.md) of the mixing device, the number of mixing protrusions in each set being defined as the number of mixing protrusions in a complete circle around the rotatable axle when seen along the direction of the rotatable axle, and wherein the minimum peripheral rotation velocity (v.sub.p,mm) of the rotary mechanism is further defined as
Vp.sub.r min=C(d.sub.md/#.sub.mp), where C is a constant equal to, or higher than, 12π, #.sub.mp is the number of the radially separated mixing protrusions in each set and d.sub.md [m] is the radial diameter of the mixing device.

4. The method according to claim 1, wherein a ratio between the radial diameter (d.sub.md) of the mixing device and a radial diameter (d.sub.c) of the treatment chamber is between 0.8 and 1.0.

5. The method according to claim 1, wherein the peripheral rotation velocity (v.sub.p) of the rotary mechanism is regulated such that an evaporated part of the substance present within the minimum peripheral volume (V.sub.p) acquires a turbulent flow characteristic.

6. The method according to claim 1, wherein the plurality of radially separated mixing protrusions is divided into one or more sets distributed axially along the rotatable axle, across the axial length (l.sub.md) of the mixing device, the number of mixing protrusions in each set being defined as the number of mixing protrusions in a complete circle around the rotatable axle when seen along the direction of the rotatable axle, and wherein the minimum peripheral rotation velocity (v.sub.p,mm) of the rotary mechanism is further defined as
V.sub.p,min=C(d.sub.md/#.sub.mp), where C is a constant equal to, or higher than, 45π, #.sub.mp is the number of the radially separated mixing protrusions in each set and d.sub.md [m] is the radial diameter of the mixing device.

7. The method according to claim 1, wherein the rotatable axle is arranged in alignment with a central axis (C.sub.TC) of the treatment chamber.

8. The method according to claim 1, wherein the heating device is oriented in the direction of the length l.sub.c of the treatment chamber.

9. The method according to claim 1, wherein the heating device further comprises: an enclosure arranged around the vessel such that a void is created between an outer surface of the vessel wall and an inner surface of the enclosure, the enclosure comprising an enclosure inlet allowing feed of heating means into the void.

10. The method according to claim 1, wherein at least a part of an outer surface of the vessel wall is provided with a plurality of outer fins.

11. The method according to claim 1, wherein the heating device is arranged at least partly within the vessel wall.

12. The method according to claim 1, wherein, when the flow (S.sub.i) is set at a constant rate, the input power to the heating device and the input power to the rotary drive are mutually adjusted such that the operational temperature (T.sub.op) within at least part of the minimum peripheral volume (V.sub.p) is achieved.

13. The method according to claim 1, wherein, when the input power to the rotary drive and the input power to the heating device are set at constant levels, the flow (S.sub.i) is adjusted such that the operational temperature (T.sub.op) within at least part of the minimum peripheral volume (V.sub.p) is achieved.

14. The method according to claim 1, wherein the separation apparatus further comprises: a temperature sensor arranged such that a temperature within or at the treatment chamber may be monitored, and a control system in signal communication with the temperature sensor, the feeding device, the rotary drive and the heating device, the control system being configured to automatically adjust at least one of the flow (S.sub.i), the input power of the rotary drive and the input power of the heating device based on the temperature measured by the temperature sensor.

15. The method according to claim 1, wherein the separation apparatus further comprises: a temperature sensor arranged such that the temperature within or at the treatment chamber may be monitored, and wherein the separation apparatus further comprises: a control system in signal communication with the temperature sensor and the feeding device, the control system being configured to automatically adjust the flow (S.sub.i) from the feeding device based on the temperature measured by the temperature sensor and wherein step D involves measuring the temperature within or at the treatment chamber, transmitting the temperature to the control system which calculates a new flow (S.sub.n) as function of the temperature, and adjusting the flow (S.sub.i) to the new flow (S.sub.n) by transmitting a signal to the feeding device.

16. The method according to claim 1, wherein the mixing device comprises: a plurality of rotary discs fixed with axial offsets to the rotatable axle, and a plurality of axially oriented elongated objects interconnecting the plurality of rotary discs.

17. The method according to claim 16, wherein each of the plurality of rotary discs displays at least one through-going opening for allowing the evaporated part to flow through during operation.

18. The method according to claim 1, wherein the mixing device comprises a plurality of radially protruding elements distributed with offsets along the length of the rotatable axle.

19. The method according to claim 18, wherein the mixing device comprises a plurality of rotary discs fixed with axial offsets to the rotatable axle and a plurality of axially oriented elongated objects interconnecting the plurality of rotary discs, wherein the plurality of radially protruding elements are replaceably connected to the plurality of axially oriented elongated objects.

20. The method according to claim 1, wherein the vessel is a cylinder having an inner axial length l.sub.c and an inner radial diameter d.sub.c, wherein the ratio between the inner axial length l.sub.c and the inner radial diameter d.sub.c is equal or less than 4.0.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0170] Following drawings are appended to facilitate the understanding of the invention. The drawings show embodiments of the invention, which will now be described by way of example only, where:

[0171] FIG. 1 is a schematic side view of a separation apparatus according to the invention.

[0172] FIG. 2 is a schematic side view of a separation assembly according to the invention.

[0173] FIG. 3 is a perspective cut-off side view of a first embodiment of a separation apparatus according to the invention.

[0174] FIG. 4 is a perspective cut-off side view of the separation apparatus of FIG. 3, wherein inner ribs are arranged on the vessel's inner surface.

[0175] FIG. 5 is a perspective cut-off front view of the separation apparatus of FIG. 3, wherein the cut-off plane is located further into the apparatus' vessel.

[0176] FIG. 6 is a perspective cut-off side view of a peripheral part of the separation apparatus shown in FIG. 3, wherein one radially protruding element is shown in further details in a separate drawing.

[0177] FIG. 7 is a perspective side view of the separation apparatus of FIG. 3-5.

[0178] FIG. 8 is a perspective cut-off side view of a second embodiment of a separation apparatus according to the invention, wherein one turbulence generating elongated object is shown in further details in a separate drawing.

[0179] FIG. 9 is a perspective cut-off side view of the separation apparatus of FIG. 8, wherein inner ribs are arranged on the vessel's inner surface.

[0180] FIG. 10 is a perspective side view of a rotary mechanism of a separation apparatus according to the invention.

DETAILED DESCRIPTION OF THE INVENTION

[0181] In the following, embodiments of the invention will be discussed in more detail with reference to the appended drawings. It should be understood, however, that the drawings are not intended to limit the invention to the subject-matter depicted in the drawings.

[0182] It is appreciated that certain features of the invention, which, for clarity, are described in the context of separate embodiments, may also be provided in combination in a single embodiment. Conversely, various features of the invention, which, for brevity, have been described in the context of a single embodiment, may also be provided separately or in any suitable sub-combination. In particular, it will be appreciated that features described in relation to one particular embodiment may be interchangeable with features described in relation to other embodiments.

[0183] With particular reference to FIG. 1 showing a first embodiment of the invention, the separation apparatus 100 is configured to perform continuous thermal separation of a substance 12 flowing into a treatment chamber 2 inside a cylindrical vessel 1 having an inner surface 1a and an outer surface 1b. The vessel includes a cylindrical wall of length l.sub.c and two circular end walls of diameter (or alternatively oval or rectangular or squared with height H and width W) arranged on each ends of the cylindrical wall.

[0184] The substance 12 fed into the substance inlet 3 by use of a feeding device 20 (FIG. 2) is composed of multi-components (A.sub.n, where n>1), where one or more of these components 12b (A.sup.e.sub.m, where m≤n) are evaporable with distinct evaporation temperatures (T.sup.e.sub.i, where i=1 . . . m). Hence, a part 12a of the substance 12 (A.sub.n-m) may be considered non-evaporable within a set operational temperature (T.sub.op≥T.sup.e.sub.i) inside the treatment chamber 2. The non-evaporable and the evaporable parts 12a, 12b are released from the vessel 1 through a first and second outlet 4, 5, respectively. During operation a vapor cloud 12c is formed comprising a mix of non-evaporable parts 12a and evaporable parts 12b. Said vapor cloud 12c includes both fluids (gas and/or liquids) and solids/particles.

[0185] The vessel 1 contains a rotatory mechanism 7 having a rotatable axle 7a aligned with a central, longitudinal axis C.sub.TC of the vessel 1. The axle 7a extends across the length l.sub.c of the vessel 1 and through at least one of the end walls, preferably both.

[0186] The rotatory mechanism 7 further includes a mixing device 7b-d fixed to the rotatable axle 7a inside the treatment chamber 2. The mixing device 7b-d comprises at least one, preferably at least two, rotary sheaves or discs 7b rigidly fixed perpendicularly onto the axle 7a and a plurality of mixing protrusions/protruding elements 7d fixed at the outer radial end of the discs 7b. In case of a plurality of discs 7b, these are arranged with spacings/offsets along the axle's 7a longitudinal direction (i.e. along axis C). In FIG. 1, a total of seven spaced-apart discs 7b are shown, where all discs except the leftmost disc displays openings 7b1 near the axle 7a, thereby allowing evaporated components 12b to flow therethrough. The main purpose of the single closed disc 7b arranged nearest the end wall displaying the substance inlet(s) 3 (see FIG. 7) is to hinder the solids from the vapor cloud 12c to enter the volume between the rotatable axle 7a and the protruding elements 7d, thereby avoiding solids to mix with evaporated parts 12b and to be released through the second outlet 5.

[0187] To further prevent solids from escaping the second outlet 5, a narrow slit composed of two circumferentially extending plates 23 have been fixed to the disc 7b nearest the second outlet 5 and the adjacent inner wall 1a, respectively.

[0188] The mixing device 7b-d further comprises a plurality of bars 7c fixed at or near the discs' 7b outer rims 7b2, where each of the bars 7c has a length and an orientation directed along (parallel with) the vessel's 1 central axis C.sub.TC which allows interconnection of two or more of the discs 7b, and preferably interconnections of all of the discs 7b.

[0189] For the first embodiment depicted in FIGS. 1-6, the mixing device 7b-d also comprises a plurality of rods 7d replaceably connected to each bar 7c such that they protrude radially towards the inner surface 1a of the vessel's 1 cylindrical wall, i.e. perpendicular to the vessel's 1 central axis C.sub.TC. The main purpose of the rods 7d is to create intense mixing of the vapor cloud 12c to enhance the heat transfer from the inner wall 1a.

[0190] With the particular configuration shown in FIG. 1, experiments show that an intense mixing of the vapor cloud 12c was achieved with a peripheral velocity v.sub.p of 34.5 m/s measured at the ends of the rods 7d closest to the inner vessel walls. During the experiments, a mixing device 7a-d with sets of eight rods 7d (#.sub.mp=8) distributed with spacings along the entire mixing device length l.sub.md. The eight rods 7d of each set is further distributed with spacings along the entire circumference of the mixing device 7b-d. The mixing device 7b-d had a diameter d.sub.md of 1.1 m and the inner vessel diameter d.sub.c was 1.2 m.

[0191] A peripheral velocity of 34.5 m/s with this particular configuration corresponds to a revolution velocity ω.sub.rev of 600 rounds per minutes (r.p.m). With eight rods 7d along the mixing device's circumference, this corresponds to 4800 sweeps per minute (s.p.m.) across a specific area of the inner vessel wall 11a.

[0192] If one decide to keep the number of sweeps constant, it can be deduced that the minimum peripheral rotation velocity at the outer radial boundary of the rods/mixing protrusions can be formulated as follows:

v.sub.p,min=80π(d.sub.md/#.sub.mp),

[0193] where d.sub.md is the diameter of the mixing device and #.sub.mp is the number of mixing protrusions.

[0194] Further experiments show that vapor cloud with turbulent characteristics can be achieved with a number of s.p.m. significantly lower than 4800, at least down to 2700 s.p.m. This corresponds to a minimum peripheral rotation velocity of

v.sub.p,min=45π(d.sub.md/#.sub.mp),

[0195] With particular reference to FIG. 6, the shape of the end 7d1 of each rod 7d situated nearest the inner surface 1a may be varied to optimize said mixing of the vapour cloud in a minimum peripheral volume V.sub.p delimited by the radial extent of the rotary mechanism 7 and the inner surface 1a. As shown in the detailed drawings within the oval frame of FIG. 6, the termination of the rod 7d may be flat, or near flat, relative to the facing inner surface 1a. However, the ends 7d1 may be of any shape as long as they contribute to the mixing of the vapor cloud 12c present in the minimum peripheral volume V.sub.p. The detailed drawing within the oval frame in FIG. 1 shows various examples of possible shapes of the ends 7d1. Note that the exemplary rods 7d within the oval frame of FIG. 1 are all turned 90° counterclockwise in respect of the rods 7d shown within the vessel 1.

[0196] To ensure rotation of the rotatory mechanism 7, and thereby also the mixing device 7b-d, an end section 7a1 of the axle 7a is connected to a rotary drive 10. As shown in FIG. 2, the latter is powered by an internal and/or external rotary motor 10a. In the exemplary configuration shown in FIG. 2, the rotary drive 10 comprises a rotary motor 10a, a transmission belt 10b and two transmission pulleys 10c arranged around the end section 7a1 and a rotatable axle of the rotary motor 10a, respectively.

[0197] The first outlet 4 is dedicated for releasing solid-state particulates (non-evaporated parts) 12a, while the second outlet 5 is dedicated for releasing the evaporated parts 12b. In order to avoid release of vapor out of the treatment chamber 2 through the first outlet 4, a rotary valve 22 (FIG. 1) is fixed to the first outlet 4, thereby discharging the non-evaporated parts 12a from the first outlet 4.

[0198] After being released from the first outlet 4 through the rotary valve 22, the non-evaporated part 12a may be collected by a dedicated solid discharge container 40 arranged below, or partly below, the vessel 1 (FIG. 2).

[0199] In order to monitor the temperature inside the vessel 1, one or more temperature sensors 19 at various locations may be arranged within or near the treatment chamber 2, for example outside or within the vessel wall and/or within the first outlet 4. The latter position is depicted in FIG. 1.

[0200] The vapor 12b may be fed into a condensing system 30. The latter may be performed in three steps: [0201] The vapor 12b is flowing into a gas scrubber to clean the vapor 12b for minor amounts of solid-state particulates. A small amount of a first liquid such as oil may also be condensed within the gas scrubber. [0202] The cleaned vapor 12b is further flowing into a liquid condenser, for example an oil condenser, to condense the first liquid from the vapor 12b. [0203] Lastly, the cleaned vapor having no or reduced amount of the first liquid (for example lighter oil) is flowing into a steam condenser which condense at least a second type of liquid such as water and, if applicable, the reduced amount of the first liquid.

[0204] In FIG. 1, the first outlet 4 and the second outlet 5 are seen arranged adjacent the end wall distal the rotary drive 10, wherein their openings out of the vessel 1 are directed along the central axis C.sub.TC and tilted down relative to the central axis C.sub.TC, respectively. However, the first and second outlets 4, 5 may be configured in any direction as long as they allow release of non-evaporated and evaporated parts 12a, 12b during operation. FIGS. 3-5 and 7 of the first embodiment and FIGS. 8-9 of the second embodiment show an alternative configuration of the first outlet 4 having a vertical opening out from the treatment chamber 2 at the vessel's 1 base.

[0205] The total radial diameter d.sub.md of the rotatory mechanism 7/mixing device 7b-d, i.e. twice the total radial length from the central axis C.sub.TC to the rotatory mechanism's 7 radial boundary, is preferably more than 90% of the diameter of the treatment chamber 2. For example, if the inner diameter d.sub.c of the cylindrical vessel 1 is 2 meters, the average distant between the end 7d1 of each plurality of rods 7d and the inner surface 1a should preferably be less than 10 cm, for example 3 or 4 cm.

[0206] In all of the exemplary configurations of FIGS. 1 and 3-9, a heating device 6 is depicted as an assembly comprising both [0207] a plurality of resistive heating elements in the shape of poles/rods 6″arranged within the vessel wall along (i.e. parallel with) the central axis C.sub.TC and [0208] a hot fluid system arranged around the cylindrical wall comprising an enclosure 13 forming a void 14 between an inner surface of the enclosure 13 and the outer surface 1b of the vessel 1. The enclosure 13 further comprises a heat inlet 13a for feeding heated fluid 6′ into the void 14 and a heat outlet 13b for releasing the heated fluid 6′ out of the void 14.

[0209] However, note that the heating device 6 may comprise any types and any number of heating mechanisms capable of heating the inner wall 1a of the vessel 1. For example, in alternative embodiments the heating device 6 may consist of only one or more resistive heating elements within and/or outside the container wall or consist of only said hot fluid system. The heating device 6 may alternatively, or in addition, comprise a microwave heater system and/or an induction heater system arranged on or near the outer surface 1b of the vessel 1 and/or inside the treatment chamber 2.

[0210] FIG. 7 shows a separation apparatus 100 where one of the end walls of the vessel 1 displays two substance inlets 3, an opening for the rotatable axle 7a and an inspection/service hatch 18. It should however be understood that this end wall may comprise any number of substance inlets 3 and any number of hatches 18. For the particular configuration shown in FIG. 7, only one of the two substance inlets 3 are used during operation. The other may be closed, for example by the same material as the remaining part of the vessel 1 or with transparent glass. Alternatively, the substance 12 may be fed through both inlets 3 during operation.

[0211] The black arrows 6′ pointing into the heat inlet 13a and out of the heat outlet 13b, respectively, symbolize the flow of hot fluid.

[0212] FIGS. 8 and 9 show a second embodiment of the separation apparatus 100. Compared to the first embodiment, the plurality of rods 7d are omitted. The rotary mechanism 7 thus comprises the rotatable axle 7a and the mixing device 7c-d, where the latter is set up by a plurality of discs 7b and interconnecting bars 7c. The desired mixing of the substance 12 within the minimum peripheral volume V.sub.p is consequently largely ensured by the longitudinally directed bars 7c.

[0213] To enable maximized mixing, preferably to the extent that the vapor cloud 12c experiences a turbulent flow characteristic within V.sub.p, the shape of the bars 7c may be optimized, for example through repeated testing in which various shapes of the bars 7c are inserted and operated, and where the heat transfer is measured during each operation. FIGS. 8-9 show one exemplary configuration of the bars 7c where the longitudinal cross-sectional area displays has a triangular shape. The sharp edges 7c1 of the triangular bar 7c may induce more turbulence in the minimum peripheral volume and intense mixing of the vapour cloud 12c.

[0214] The above described separation apparatus 100 enables effective removal of liquids and/or gases from a substance 12 by thermal separation, using for example waste heat 6′ as the main indirect energy for separation of waste and bi-products. Due to the combined external heating of the vessel 1 and the fierce mixing of the substance components/vapor cloud 12c, the separation apparatus 100 can operate continuously without the presence of a net internal transport mechanism causing a gradual heating of the substance 12 (as necessary in the currently known indirect separation methods).

[0215] By use of the above described apparatus 100, the heat is not transferred mainly to the solids in the waste, as case is for indirect separation methods. Instead, the heat is transferred to the vapor cloud 12c having much higher heat transfer coefficient. This vapor cloud 12c is composed of mainly (by volume) evaporated liquids/gases, and also hot non-evaporated particles. If water is present in the incoming substance 12, the ‘evaporated’ vapor cloud 12c will necessarily contain steam.

[0216] During operation, the following process steps take place: [0217] The heating device 6 and the rotary mechanism 7 cause the incoming substance 12 to transform into a vapor cloud 12c. [0218] The thermal energy from the heating device 6 is transferred from the inner surface 1a of the vessel 1 to the generated vapor cloud 12c. [0219] The thermal energy is subsequently transferred from this heated vapor cloud 12c onto the incoming substance 12 by intense mixing/turbulence from the rotary mechanism 7.

[0220] The heat transfer from steel to a dried solid typically found in prior art indirect heating separators is experienced to be ca. 75 W/m.sup.2K. In comparison, the heat transfer from steel to steam (which will be a typical main ingredient of the vapor cloud 12c during thermal separation of waste) is significantly higher, typically ca. 6000 W/m.sup.2K.

[0221] Hence, by heating the substance 12 via the above-mentioned heating steps the inventive apparatus achieves a heat transfer capacity significantly higher than 75 W/m.sup.2K (but below 6000 W/m.sup.2K).

[0222] The final heat transfer will depend inter alia on the water content. For example, a heat transfer coefficient between 1000 and 1200 W/m.sup.2K has been verified when thermal separation tests have been performed on a substance containing approx. 15% water, 15% oil and 70% non-evaporable substance (by weight). The latter is typical composition for cuttings after drilling operations.

[0223] As mentioned above, the intense mixing/turbulence mechanism will secure an optimal mixing and heat exchange from the vapor cloud 12c onto the continuously fed substance 12 through the substance inlet 3 and the various components in this substance, thereby causing an almost instant evaporation of in particular liquids within the substance 12. The vessel 1 will thereby—at all times—contain a vapor cloud 12c with optimal heat transfer capabilities, both from the inner surface 1a as well as onto the incoming substance 12.

[0224] Although particles in any created vapor cloud will necessarily be forced to the periphery of the treatment chamber by centrifugal forces, the continuous evaporation of liquids (such as water) will create strong internal forces in all internal directions, thereby securing a high percentage of vapor (steam) at the periphery.

[0225] Tests with the inventive separation apparatus has been performed while treating a waste substance containing 70% mineral solids, 15% water and 15% oil by weight (cuttings from drilling operations). The tests demonstrated a heat transfer rate between approx. 1000 W/m.sup.2K and 1200 W/m.sup.2K. Even higher heat transfer rates are expected for substances containing more water.

[0226] In the preceding description, various aspects of the method and the apparatus according to the invention have been described with reference to the illustrative embodiment. For purposes of explanation, specific numbers, systems and configurations were set forth in order to provide a thorough understanding of the apparatus and its workings. However, this description is not intended to be construed in a limiting sense. Various modifications and variations of the illustrative embodiments, as well as other embodiments of the method and the apparatus, which are apparent to persons skilled in the art to which the disclosed subject matter pertains, are deemed to lie within the scope of the present invention.